CA1092821A - Method of operating a coal gasifier - Google Patents
Method of operating a coal gasifierInfo
- Publication number
- CA1092821A CA1092821A CA301,007A CA301007A CA1092821A CA 1092821 A CA1092821 A CA 1092821A CA 301007 A CA301007 A CA 301007A CA 1092821 A CA1092821 A CA 1092821A
- Authority
- CA
- Canada
- Prior art keywords
- coal
- zone
- combustion
- gasifier
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 239000003245 coal Substances 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims description 8
- 238000002485 combustion reaction Methods 0.000 claims description 16
- 238000002309 gasification Methods 0.000 claims description 10
- 238000011144 upstream manufacturing Methods 0.000 claims 6
- 238000010304 firing Methods 0.000 claims 2
- 239000007789 gas Substances 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 10
- 239000002245 particle Substances 0.000 description 3
- 230000007423 decrease Effects 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000155 melt Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/466—Entrained flow processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/50—Fuel charging devices
- C10J3/503—Fuel charging devices for gasifiers with stationary fluidised bed
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/52—Ash-removing devices
- C10J3/523—Ash-removing devices for gasifiers with stationary fluidised bed
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0956—Air or oxygen enriched air
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S48/00—Gas: heating and illuminating
- Y10S48/02—Slagging producer
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Solid-Fuel Combustion (AREA)
- Solid Fuels And Fuel-Associated Substances (AREA)
- Crucibles And Fluidized-Bed Furnaces (AREA)
- Industrial Gases (AREA)
Abstract
Abstract of the Disclosure An entrained flow coal gasifier having two levels of coal introduction in the combustor portion. Load is reduced by operating the lower level of coal at approximately stoichiometric conditions while increasing substoichiometry of the upper level.
Cs 3473
Cs 3473
Description
2~3Zi Background of the Invention This invention relates to entrained flow coal gasifiers and in particular to a method of operating such gasifiers through a load range.
The entrained flow gasifier is essentially comprised of two zones. The f;rst or the combustion zone generates the heat required for the gasification process. This zone is operated at near stoichiometric conditions to obtain the maximum heat and also to melt the ash so that it may be removed in the form of slag. The operation of this zone is off stoichiometric only to the extent required to reduce temperature where the materials forming the combustion zone cannot tolerate stoichio-metric temperature.
The combustion products from the combustor zone are then mixed with incoming pulverized coal. The incoming coal is devolatilized and the carbon particles combine with the combustion products to form a gas which is largely carbon monoxide. This is an endothermic reaction ob-taining its heat from the gases leaving the combustor. The gasification process continues until the temperature is reduced to a level at which the gasification rate is too slow for practical operation. Any remaining coal particles in the form of char may be recycled to the combustor.
After a gasifier is designed for optimum conditions at the maximum rating the same gasifier must be operated at reduced ratings.
In such an operation the coal and air to the combustor is reduced while still maintaining stoichiometric conditions therein. Similarly the coal supplied to the reductor section is reduced in accordance with the reduced gas flow.
Summary of the Invention It is an object of the invention to increase the effectiveness of a gasifier when operating at reduced ratings.
In accordance with the invention, the combustor is fired at two levels. Load is reduced while maintaining stoichiometric proportions of Cs 3473 -2-109;~8~21 air and fuel at the lower nozzle, thereby effecting the maximum gas temperature and the most effective slagging conditions. The coal and air supply at the upper level of nozzles in the combustor are modified so that the ratio becomes increasingly substoichiometric as load is reduced. Accordingly, a portion of the gasifying reaction which normally would occur in the reductor is obtained in the combustor. Actually by forcing the reaction to take place lower at low load we cause the gas making reaction to take place before the heat is absorbed by upper water walls increasing the heating level of gas and reducing the leaving temperature accordingly.
Brief Description of the Drawing The figure is a schematic illustration of a gasifier.
Descri tion of the Preferred Embodiment p A gasifier generally indicated as 10 is formed of surrounding walls 12 formed of steam generating tubes. Water is supplied to the lower header 14 and exits throush the upper header 15. Steam may be generated in these circuits to perform useful work.
Coal from bin 18 is supplied to a lower level of coal nozzles 20 through feeder 22. These nozzles are located at a plurality of locations around the combustor zone 24 and oriented for tangential introduction of coal therein. Lower wind box 26 similarly surrounds the combustor and supplies air which may be controlled in accordance with the coal passing through nozzle 20 by means of damper 2~. The air is supplied by forced draft fan 30, although oxygen enriched air or pure oxygen may be used.
Additional coal may be supplied through feeder 32 to nozzles 34. A second wind box 36 surrounds the combustor in a location to supply air as desired in conjunction with coal nozzles 34. This air may be controlled by damper 3~.
The ratio of air and fuel to the combustor 24 is maintained as near stoichiometric as possible considering the ability of the structural materials to withstand the temperature. Ash melts in the Cs~;3473 ':
109'~82~
combustor and is removed throug~ slag spout 40. The combust;on products pass upwardly into reductor zone 42. In this zone additional coal is ;ntroduced through nozzles 44 in amounts controlled by feeder 46. This coal is devolatilized and gasified while undergoing an endothermic reaction with the combustion products from the combustor 24. Accordingly a low BTU
gas is formed which exits through line 48. The gas passes through a dust collector 50 with the gas passing outwardly through line 52 for clean-up and use. Portions of the coal in the form of char are collected in dust collector S0 and returned through line 54 and feeder 56. These char particles are introduced through nozzles 58 into the lower portion of the combustor at a location similar to the introduction of coal through nozzles 20.
The gasifier is designed so that at the full load sufficient heat is generated in combustor 24 to satisfy the endothermic reaction.
A portion of this heat is transfered to the walls. This heat transfer is a function of the temperature level of the gases at each location through the gasifier. The gasifier is also sized so that the exit temperature from reductor section 42 is aboutl700 F at which point the rate of gasification is small.
~Jhen the output of this gasifier must be decreased the coal and/or char through nozzles 20 and 58 are maintained in proportion to the air flowing through wind box 26 to maintain near stoichiometric conditions in the lower portion of the combustor 24. The maximum temperature and most effective slagging conditions are thereby obtained. The maximum temperature is also available for the gasification reaction. The upper level of coal nozzles 34 are regulated in proportion to the air passing through wind box 36 in such a manner as to form substoichiometric conditions in the upper portion of the combustor 24. A portion of the gasification is thereby accomplished in the combustor with the concomitant endothermic reaction. This decreases the gas temperature in that area and accordingly it decreases the heat loss to the walls. It follows that since less heat is lost to the walls, more is available for the gasification reaction. As Cs 3473 A
` 1~9;~821 .
the combustion products flow up into the reductor zone 42 additional coal is supplied through nozzles 44 in an amount required to complete the gasification reaction.
What is claimed is:
Cs 3473 -5
The entrained flow gasifier is essentially comprised of two zones. The f;rst or the combustion zone generates the heat required for the gasification process. This zone is operated at near stoichiometric conditions to obtain the maximum heat and also to melt the ash so that it may be removed in the form of slag. The operation of this zone is off stoichiometric only to the extent required to reduce temperature where the materials forming the combustion zone cannot tolerate stoichio-metric temperature.
The combustion products from the combustor zone are then mixed with incoming pulverized coal. The incoming coal is devolatilized and the carbon particles combine with the combustion products to form a gas which is largely carbon monoxide. This is an endothermic reaction ob-taining its heat from the gases leaving the combustor. The gasification process continues until the temperature is reduced to a level at which the gasification rate is too slow for practical operation. Any remaining coal particles in the form of char may be recycled to the combustor.
After a gasifier is designed for optimum conditions at the maximum rating the same gasifier must be operated at reduced ratings.
In such an operation the coal and air to the combustor is reduced while still maintaining stoichiometric conditions therein. Similarly the coal supplied to the reductor section is reduced in accordance with the reduced gas flow.
Summary of the Invention It is an object of the invention to increase the effectiveness of a gasifier when operating at reduced ratings.
In accordance with the invention, the combustor is fired at two levels. Load is reduced while maintaining stoichiometric proportions of Cs 3473 -2-109;~8~21 air and fuel at the lower nozzle, thereby effecting the maximum gas temperature and the most effective slagging conditions. The coal and air supply at the upper level of nozzles in the combustor are modified so that the ratio becomes increasingly substoichiometric as load is reduced. Accordingly, a portion of the gasifying reaction which normally would occur in the reductor is obtained in the combustor. Actually by forcing the reaction to take place lower at low load we cause the gas making reaction to take place before the heat is absorbed by upper water walls increasing the heating level of gas and reducing the leaving temperature accordingly.
Brief Description of the Drawing The figure is a schematic illustration of a gasifier.
Descri tion of the Preferred Embodiment p A gasifier generally indicated as 10 is formed of surrounding walls 12 formed of steam generating tubes. Water is supplied to the lower header 14 and exits throush the upper header 15. Steam may be generated in these circuits to perform useful work.
Coal from bin 18 is supplied to a lower level of coal nozzles 20 through feeder 22. These nozzles are located at a plurality of locations around the combustor zone 24 and oriented for tangential introduction of coal therein. Lower wind box 26 similarly surrounds the combustor and supplies air which may be controlled in accordance with the coal passing through nozzle 20 by means of damper 2~. The air is supplied by forced draft fan 30, although oxygen enriched air or pure oxygen may be used.
Additional coal may be supplied through feeder 32 to nozzles 34. A second wind box 36 surrounds the combustor in a location to supply air as desired in conjunction with coal nozzles 34. This air may be controlled by damper 3~.
The ratio of air and fuel to the combustor 24 is maintained as near stoichiometric as possible considering the ability of the structural materials to withstand the temperature. Ash melts in the Cs~;3473 ':
109'~82~
combustor and is removed throug~ slag spout 40. The combust;on products pass upwardly into reductor zone 42. In this zone additional coal is ;ntroduced through nozzles 44 in amounts controlled by feeder 46. This coal is devolatilized and gasified while undergoing an endothermic reaction with the combustion products from the combustor 24. Accordingly a low BTU
gas is formed which exits through line 48. The gas passes through a dust collector 50 with the gas passing outwardly through line 52 for clean-up and use. Portions of the coal in the form of char are collected in dust collector S0 and returned through line 54 and feeder 56. These char particles are introduced through nozzles 58 into the lower portion of the combustor at a location similar to the introduction of coal through nozzles 20.
The gasifier is designed so that at the full load sufficient heat is generated in combustor 24 to satisfy the endothermic reaction.
A portion of this heat is transfered to the walls. This heat transfer is a function of the temperature level of the gases at each location through the gasifier. The gasifier is also sized so that the exit temperature from reductor section 42 is aboutl700 F at which point the rate of gasification is small.
~Jhen the output of this gasifier must be decreased the coal and/or char through nozzles 20 and 58 are maintained in proportion to the air flowing through wind box 26 to maintain near stoichiometric conditions in the lower portion of the combustor 24. The maximum temperature and most effective slagging conditions are thereby obtained. The maximum temperature is also available for the gasification reaction. The upper level of coal nozzles 34 are regulated in proportion to the air passing through wind box 36 in such a manner as to form substoichiometric conditions in the upper portion of the combustor 24. A portion of the gasification is thereby accomplished in the combustor with the concomitant endothermic reaction. This decreases the gas temperature in that area and accordingly it decreases the heat loss to the walls. It follows that since less heat is lost to the walls, more is available for the gasification reaction. As Cs 3473 A
` 1~9;~821 .
the combustion products flow up into the reductor zone 42 additional coal is supplied through nozzles 44 in an amount required to complete the gasification reaction.
What is claimed is:
Cs 3473 -5
Claims (4)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A method of operating an entrained flow coal gasifier comprising: firing coal at two levels in a combustion zone with near stoichiometric air; removing molten ash from said combustion zone; conveying combustion products upwardly from said combustion zone through a reduction zone; injecting additional coal into the combustion products in said reduction zone and gasifying at least a portion of the coal to form low BTU gas; conveying the gas to a point of use; including also reducing gasifier output by, modifying the ratio of air to coal supplied to the upper level of the combustion zone 50 that the ratio becomes increasingly substoichiometric thereby extending the gasification of coal from the reduction zone into the upper level of the combustion zone; and maintaining the lower level of coal in the combustion zone at near stoichiometric conditions so as to provide sufficient heat to maintain effective slagging conditions
2. The method as in claim 1 wherein at least a portion of the coal fired to said combustor is in the form of char.
3. In a method operating an entrained flow coal gasifier comprising: firing coal at two levels in an upstream zone with near stoichiometric air at each level; removing molten ash from said upstream zone; conveying combustion products upwardly from said upstream zone through a downstream reduction zone; injecting additional coal into the combustion products in said downstream zone and gasifying at least a portion of the coal to form low BTU gas; conveying the gas to a point of use; the improvement comprising modifying the ratio of air to coal supplied to the upper level of the upstream zone so that the ratio becomes increasingly substoichiometric as the gas output of the gasifier is reduced, thereby extending the gasification of coal from the downstream reduction zone into the upper level of the upstream zone; and maintaining the lower level of coal in the upstream zone at near stoichiometric conditions so as to provide sufficient heat to maintain effective slagging conditions.
4. The method as in claim 3 wherein at least a portion of the coal fired to said combustor is in the form of char.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US825,492 | 1977-08-18 | ||
| US05/825,492 US4168956A (en) | 1977-08-18 | 1977-08-18 | Method of operating a coal gasifier |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1092821A true CA1092821A (en) | 1981-01-06 |
Family
ID=25244137
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA301,007A Expired CA1092821A (en) | 1977-08-18 | 1978-04-12 | Method of operating a coal gasifier |
Country Status (15)
| Country | Link |
|---|---|
| US (1) | US4168956A (en) |
| JP (1) | JPS5432508A (en) |
| AU (1) | AU513999B2 (en) |
| BE (1) | BE867168A (en) |
| CA (1) | CA1092821A (en) |
| DE (1) | DE2819419C3 (en) |
| ES (1) | ES469667A1 (en) |
| FR (1) | FR2400550A1 (en) |
| GB (1) | GB1591082A (en) |
| IN (1) | IN147196B (en) |
| IT (1) | IT1096220B (en) |
| NL (1) | NL7805325A (en) |
| SE (1) | SE7805607L (en) |
| YU (1) | YU117678A (en) |
| ZA (1) | ZA782825B (en) |
Families Citing this family (45)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2947222C2 (en) * | 1979-11-23 | 1987-05-07 | Carbon Gas Technologie GmbH, 4030 Ratingen | Device for gasification of solid, dusty to lumpy carbonaceous fuels and their use |
| EP0050863A1 (en) * | 1980-10-24 | 1982-05-05 | Hitachi, Ltd. | Process of and apparatus for gasifying coals |
| JPS57139184A (en) * | 1981-02-23 | 1982-08-27 | Hitachi Ltd | Coal gasification |
| JPS5776088A (en) * | 1980-10-31 | 1982-05-12 | Nippon Kokan Kk <Nkk> | Coal gasification using powdered coal and its device |
| US4343627A (en) * | 1980-11-28 | 1982-08-10 | Combustion Engineering, Inc. | Method of operating a two-stage coal gasifier |
| US4319888A (en) * | 1980-12-12 | 1982-03-16 | Combustion Engineering, Inc. | Apparatus for mixing char-ash into coal stream |
| JPS57182395A (en) * | 1981-05-06 | 1982-11-10 | Hitachi Ltd | Apparatus for gasification of coal |
| FI62554C (en) * | 1981-05-22 | 1983-01-10 | Ahlstroem Oy | FARING EQUIPMENT FOR ORGANIZATION OF FAST KOLHALTIGT MATERIAL |
| JPH0649874B2 (en) * | 1982-08-25 | 1994-06-29 | 株式会社日立製作所 | Coal spouted bed gasification method |
| JPS5984980A (en) * | 1982-11-04 | 1984-05-16 | Hitachi Ltd | Coal gasification apparatus |
| US4489562A (en) * | 1982-11-08 | 1984-12-25 | Combustion Engineering, Inc. | Method and apparatus for controlling a gasifier |
| JPS59172589A (en) * | 1983-03-23 | 1984-09-29 | Hitachi Ltd | Coal gasification method |
| JPS59176391A (en) * | 1983-03-28 | 1984-10-05 | Hitachi Ltd | coal gasifier |
| JPS6065094A (en) * | 1983-09-20 | 1985-04-13 | Babcock Hitachi Kk | Spouted bed coal gasifying oven |
| JPS60208396A (en) * | 1984-04-02 | 1985-10-19 | Hitachi Ltd | Method of gasification of coal |
| JPS612426U (en) * | 1984-06-13 | 1986-01-09 | 財団法人 電力中央研究所 | gasifier combustor |
| US4569680A (en) * | 1984-12-26 | 1986-02-11 | Combustion Engineering | Gasifier with economizer gas exit temperature control |
| JPS61207493A (en) * | 1985-03-13 | 1986-09-13 | Mitsubishi Heavy Ind Ltd | Coal gasifying apparatus |
| JPH0823028B2 (en) * | 1985-03-13 | 1996-03-06 | 三菱重工業株式会社 | Coal gasifier |
| JPS61218690A (en) * | 1985-03-25 | 1986-09-29 | Mitsubishi Heavy Ind Ltd | Coal gasifier |
| JPH0631347B2 (en) * | 1985-03-26 | 1994-04-27 | 三菱重工業株式会社 | Coal gasifier |
| JPS61228093A (en) * | 1985-04-01 | 1986-10-11 | Mitsubishi Heavy Ind Ltd | Fuel gasification apparatus |
| JPS61243895A (en) * | 1985-04-23 | 1986-10-30 | Mitsubishi Heavy Ind Ltd | Pressure spouted bed gasification oven |
| JPS61246287A (en) * | 1985-04-24 | 1986-11-01 | Mitsubishi Heavy Ind Ltd | Spouted bed coal gasification oven |
| JPS61181679U (en) * | 1985-05-04 | 1986-11-12 | ||
| CN1010028B (en) * | 1985-05-29 | 1990-10-17 | 国际壳牌研究有限公司 | Gas reactor for lignites |
| US4872886A (en) * | 1985-11-29 | 1989-10-10 | The Dow Chemical Company | Two-stage coal gasification process |
| IN168599B (en) * | 1985-11-29 | 1991-05-04 | Dow Chemical Co | |
| US4680035A (en) * | 1986-03-27 | 1987-07-14 | Combustion Engineering, Inc. | Two stage slagging gasifier |
| JPS63238282A (en) * | 1987-03-25 | 1988-10-04 | Nec Corp | Thin lithium niobate film and production thereof |
| DE3837587C1 (en) * | 1988-11-05 | 1990-05-23 | Krupp Koppers Gmbh, 4300 Essen, De | |
| JP2719424B2 (en) * | 1989-10-10 | 1998-02-25 | デステック・エナジー・インコーポレーテッド | Coal gasification method and apparatus |
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| WO2012151625A1 (en) | 2011-05-09 | 2012-11-15 | Hrl Treasury (Idgcc) Pty Ltd | Improvements in integrated drying gasification |
| JP5816770B1 (en) * | 2015-05-22 | 2015-11-18 | 新日鉄住金エンジニアリング株式会社 | Operation method of coal gasification system |
| JP6637797B2 (en) * | 2016-03-11 | 2020-01-29 | 三菱日立パワーシステムズ株式会社 | Carbon-containing raw material gasification system and method for setting oxidizing agent distribution ratio |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US901232A (en) * | 1908-05-07 | 1908-10-13 | Byron E Eldred | Process of producing gas. |
| US1039398A (en) * | 1910-02-14 | 1912-09-24 | Allis Chalmers | Process of producing gas. |
| DE1017314B (en) * | 1953-10-09 | 1957-10-10 | Basf Ag | Process for the generation of fuel gases from dust-like to coarse-grained fuels |
| DE1125108B (en) * | 1958-06-21 | 1962-03-08 | Sumitomo Chemical Co | Process for the automatic control of the feed of the reactants to a coal dust suspension gasification device |
| US3840353A (en) * | 1971-07-30 | 1974-10-08 | A Squires | Process for gasifying granulated carbonaceous fuel |
| US3782913A (en) * | 1972-03-23 | 1974-01-01 | Us Interior | Two-stage gasification of coal with forced reactant mixing and steam treatment of recycled char |
| US3971635A (en) * | 1974-12-23 | 1976-07-27 | Gulf Oil Corporation | Coal gasifier having an elutriated feed stream |
| US3981690A (en) * | 1975-01-15 | 1976-09-21 | The United States Of America As Represented By The United States Energy Research And Development Administration | Agglomerating combustor-gasifier method and apparatus for coal gasification |
-
1977
- 1977-08-18 US US05/825,492 patent/US4168956A/en not_active Expired - Lifetime
-
1978
- 1978-04-12 CA CA301,007A patent/CA1092821A/en not_active Expired
- 1978-04-20 IN IN434/CAL/78A patent/IN147196B/en unknown
- 1978-05-03 DE DE2819419A patent/DE2819419C3/en not_active Expired
- 1978-05-10 ES ES469667A patent/ES469667A1/en not_active Expired
- 1978-05-16 YU YU01176/78A patent/YU117678A/en unknown
- 1978-05-16 SE SE7805607A patent/SE7805607L/en unknown
- 1978-05-17 AU AU36195/78A patent/AU513999B2/en not_active Expired
- 1978-05-17 FR FR7814544A patent/FR2400550A1/en active Granted
- 1978-05-17 NL NL7805325A patent/NL7805325A/en not_active Application Discontinuation
- 1978-05-17 BE BE187773A patent/BE867168A/en unknown
- 1978-05-17 IT IT23487/78A patent/IT1096220B/en active
- 1978-05-17 GB GB20205/78A patent/GB1591082A/en not_active Expired
- 1978-05-17 ZA ZA00782825A patent/ZA782825B/en unknown
- 1978-08-15 JP JP9875378A patent/JPS5432508A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| FR2400550A1 (en) | 1979-03-16 |
| IT7823487A0 (en) | 1978-05-17 |
| DE2819419C3 (en) | 1980-08-14 |
| GB1591082A (en) | 1981-06-10 |
| BE867168A (en) | 1978-09-18 |
| AU513999B2 (en) | 1981-01-15 |
| FR2400550B1 (en) | 1980-10-24 |
| JPS5432508A (en) | 1979-03-09 |
| SE7805607L (en) | 1979-02-19 |
| DE2819419B2 (en) | 1979-12-06 |
| DE2819419A1 (en) | 1979-03-01 |
| ZA782825B (en) | 1979-05-30 |
| YU117678A (en) | 1982-10-31 |
| US4168956A (en) | 1979-09-25 |
| IN147196B (en) | 1979-12-15 |
| IT1096220B (en) | 1985-08-26 |
| AU3619578A (en) | 1979-11-22 |
| NL7805325A (en) | 1979-02-20 |
| ES469667A1 (en) | 1979-01-16 |
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